EP2015013A2 - Procédé et dispositif de production d'un gaz sous pression par séparation cryogénique d'air - Google Patents

Procédé et dispositif de production d'un gaz sous pression par séparation cryogénique d'air Download PDF

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Publication number
EP2015013A2
EP2015013A2 EP08012218A EP08012218A EP2015013A2 EP 2015013 A2 EP2015013 A2 EP 2015013A2 EP 08012218 A EP08012218 A EP 08012218A EP 08012218 A EP08012218 A EP 08012218A EP 2015013 A2 EP2015013 A2 EP 2015013A2
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Prior art keywords
air stream
stream
air
pressure column
pressure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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EP08012218A
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German (de)
English (en)
Inventor
Dietrich Rottmann
Christian Kunz
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Linde GmbH
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Linde GmbH
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Publication of EP2015013A2 publication Critical patent/EP2015013A2/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude oxygen"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"

Definitions

  • the invention relates to a method for producing gaseous pressure oxygen by cryogenic separation of air according to the preamble of patent claim 1.
  • the distillation column system of the invention may be designed as a two-column system (for example as a classical Linde double column system), or as a three-column or multi-column system.
  • other means may be provided for recovering other air components, particularly noble gases, such as argon or krypton-xenon recovery.
  • the invention relates to a process in which at least one gaseous pressure product is recovered by withdrawing a liquid product stream from the nitrogen-oxygen separation distillation column system, raising it to an elevated pressure in the liquid state, and evaporating it under this increased pressure by indirect heat exchange or (at supercritical pressure) is pseudo-evaporated.
  • Such internal compression methods are known, for example DE 830805 .
  • EP 1139046 A1 EP 1146301 A1 .
  • EP 1150082 A1 EP 1213552 A1 .
  • EP 1357342 A1 or DE 10238282 A1
  • first air stream In heat exchange with the (pseudo) evaporating product stream is usually a part of the feed air (here called "first air stream") condensed or pseudo-condensed and after expansion in a throttle valve or a liquid liquid in the high pressure column and / or the low pressure column of the distillation column Systems fed.
  • This liquid supplied air reduces the amount of vaporous air, which is pre-decomposed in the high-pressure column and thereby weakens the rectification.
  • a smaller amount of liquid nitrogen which is required as the reflux liquid in the high-pressure column and the low-pressure column, is obtained in comparison to processes with gaseous feed of the total air.
  • the invention has for its object to make such a method and a corresponding device economically particularly favorable.
  • the entire condensed in the context of internal compression air is vaporized in the indirect heat exchange with the gaseous stream from the upper portion of the high pressure column.
  • the vaporized air is warmed in particular in the main heat exchanger, in which the feed air is cooled and the product stream (pseudo) is evaporated and warmed. Subsequently, it is separately brought to a suitable pressure in the recompressor to feed it into the air line.
  • the recompressed air quantity now participates in the rectification in the high-pressure column.
  • the gaseous stream is preferably formed by nitrogen from the top of the high pressure column. This is condensed against the evaporating air and can be used in high pressure column and / or low pressure column as reflux. So much reflux remains in the high-pressure column that the additional air quantity can be rectified to a high N 2 purity in the high-pressure column. The remainder serves as an additional reflux in the low-pressure column and thus improves the rectification there.
  • the indirect heat exchange of the first air stream with the gaseous stream from the upper section of the high pressure column is performed in a secondary condenser.
  • a "secondary condenser” is understood here as a condenser-evaporator separate from other heat exchangers, through which no further fluids flow.
  • a second air flow which is formed by a part of the feed air stream, is expanded in a work-performing manner and at least part of the mechanical energy generated is used to drive the recompressor.
  • no energy needs to be imported for the recompression of the first air flow as in a motor drive or in the off EP 752566 B1 known recompression in the main air compressor would be the case.
  • the invention also relates to a device for the production of gaseous pressure product by cryogenic separation of air according to claim 7.
  • the main air compressor is in FIG. 1 not shown, nor the subsequent cleaning device.
  • the compressed in the main air compressor to a second pressure of 5.5 to 15 bar, preferably about 9 bar and then compressed feed air stream 1 is a first part 2 as direct air flow through the lines 3, 5, 6 and the main heat exchanger 4 in the high pressure column 7 a Destarriulen system introduced, which also has a low-pressure column 8 and a main condenser 9.
  • the operating pressures are 5.5 to 15 bar, preferably about 9 bar in the high pressure column and 1.3 to 6 bar, preferably about 3.5 bar in the low pressure column (each at the top).
  • a second part 10 of the feed air stream 1 is recompressed in a first after-compressor 11 with aftercooler 12 to a second pressure of 30 to 50 bar, preferably about 40 bar.
  • Part 14 of the compressed air after the second pressure forms the "first air flow”.
  • This is in a second after-compressor 15 with aftercooler 16th further compressed to a third pressure (the "high pressure") of 40 to 80 bar, preferably about 60 bar.
  • the first air flow to the warm end of the main heat exchanger 4 is conducted there cooled and (pseudo) condensed.
  • the cold high-pressure air 18 is completely vaporized after throttle relaxation to 3.5 to 9.5 bar, preferably about 6 bar in a secondary condenser 20 and returned via line 22 to the cold end of the main heat exchanger 4.
  • the warmed first air stream is recompressed according to the invention in a recompressor 24 with aftercooler 25 to the first pressure and combined with the direct air stream 2.
  • Another part 27 of the air 13 under the second pressure forms the "second airflow".
  • This is cooled in the main heat exchanger 4 only to an intermediate temperature and then flows through line 28 to a relaxation machine 29, which is formed in the embodiment as a turbo-expander. There he is working to be relaxed to about the first pressure.
  • the expanded second air stream 30 flows together with the direct air stream 5 via line 6 to the high pressure column. 7
  • liquid crude oxygen 31 is withdrawn, cooled in a subcooling countercurrent 32 and fed via line 33 and throttle valve 34 of the low pressure column 8 at an intermediate point.
  • Liquid impure nitrogen 35 is taken from the high pressure column 7 at an intermediate point, also cooled in the subcooling countercurrent 32 and fed via line 36 and throttle valve 37 to the top of the low pressure column 7.
  • Gaseous nitrogen head 38 of the low pressure column 8 is substantially completely condensed to a first part 39 in the main condenser.
  • the condensate formed is returned via line 40 to the head of the high pressure column.
  • a second part 41 is substantially completely condensed in the secondary condenser in indirect heat exchange with the first air flow.
  • the condensate formed is returned via line 42 to the head of the high pressure column.
  • a third part 43 of the gaseous top nitrogen 38 of the high-pressure column 7 is warmed in the main heat exchanger 4 to approximately ambient temperature and discharged via line 44 as a gaseous nitrogen product under medium pressure.
  • gaseous impurity nitrogen is withdrawn from the head of the low pressure column 8 and withdrawn after heating in the subcooling countercurrent 32 and in the main heat exchanger 4 via line 46.
  • He can, for example, in one Evaporative cooler or be used in the cleaning device, not shown as a regeneration gas.
  • Liquid oxygen 47 is withdrawn as "liquid product stream" from the bottom of the low pressure column, brought in an oxygen pump 48 to a pressure of 50 to 100 bar, preferably about 30 bar, passed via line 49 to the main heat exchanger 4, there (pseudo-) evaporated and warmed to about ambient temperature and finally withdrawn via line 50 as a gaseous product stream.
  • liquid nitrogen 21 is withdrawn from the top of the high-pressure column 7 (or alternatively from the main condenser 9) as a further "liquid product stream", brought in a nitrogen pump 51 to a pressure of 50 to 30 bar, preferably about 100 bar, via line 52nd led to the main heat exchanger 4, there (Pseudo-) evaporated and warmed to about ambient temperature and finally withdrawn via line 53 as another gaseous product stream.
  • the high-pressure column 7 is removed via line 54 gaseous impurity nitrogen, warmed and withdrawn via line 55.
  • the expansion machine 29 and the recompressor 24 are mechanically coupled via a common well.
  • FIG. 2 also differs by the line 156 with throttle valve 157 of FIG. 1 , As a result, in addition to the first air stream 18, a portion of the raw liquid oxygen from the bottom of the high-pressure column 7 in the evaporation chamber of the Sub-condenser 20 passed. As a result, can be condensed correspondingly more nitrogen 41/42.
  • FIG. 3 based on FIG. 1 and also shows the two-stage recompression 24/124 of FIG. 2 ,
  • the entire air flow 10 is compressed in the secondary compressor 11 to the high pressure.
  • the division of turbine air 128 and first air flow 18 is performed first at the intermediate temperature of the main heat exchanger 4. This results in a correspondingly higher inlet pressure at the expansion machine 29.
  • FIG. 4 based on FIG. 2 and also has a crude argon column 458 as a first stage of argon recovery.
  • liquid oxygen is withdrawn from the bottom of the low-pressure column 8 as a liquid product (LOX).
  • the liquid reflux 435, 436, 437 for the low-pressure column 8 is here deducted from the head of the high-pressure column 7. Accordingly, gaseous impure nitrogen 445/446 is taken from an intermediate point of the low-pressure column 8 here.
  • the pure nitrogen head 461 of the low pressure column 8 is also warmed and withdrawn via line 462 as a product.
  • FIG. 5 deviates from it FIG. 4 from that the recompressor 524 is not coupled to the expansion machine 29, but is driven externally.
  • the recompressor 524 is preferably formed in two stages here.
  • the turbine booster 563 is used here to further increase the pressure in the second air stream 27, the turbine air flow.
  • the relaxation machine 629 of the FIG. 6 relaxed to about the operating pressure of the low pressure column.
  • the working expanded second air stream 630 is introduced into the low pressure column 8. For the rest, the procedure of FIG. 6 with that of the FIG. 4 match.
EP08012218A 2007-07-07 2008-07-07 Procédé et dispositif de production d'un gaz sous pression par séparation cryogénique d'air Withdrawn EP2015013A2 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102007031759A DE102007031759A1 (de) 2007-07-07 2007-07-07 Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft

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EP2600090A1 (fr) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
WO2015014485A3 (fr) * 2013-08-02 2015-09-24 Linde Aktiengesellschaft Procédé et dispositif de production d'azote comprimé
EP2963369A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2963371A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
EP2963370A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
WO2016005031A1 (fr) 2014-07-05 2016-01-14 Linde Aktiengesellschaft Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable
WO2020169257A1 (fr) 2019-02-22 2020-08-27 Linde Gmbh Procédé et installation de décomposition d'air à basse température
WO2021242308A1 (fr) * 2020-05-26 2021-12-02 Praxair Technology, Inc. Améliorations apportées à une unité de séparation d'air cryogénique à double colonne produisant de l'azote
US11674750B2 (en) 2020-06-04 2023-06-13 Praxair Technology, Inc. Dual column nitrogen producing air separation unit with split kettle reboil and integrated condenser-reboiler
US11933540B2 (en) 2020-06-04 2024-03-19 Praxair Technology, Inc. Dual column nitrogen producing air separation unit with split kettle reboil and integrated condenser-reboiler

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